CN113457852A - Flotation method for high-oxidation-rate peat plash lead-zinc ore - Google Patents
Flotation method for high-oxidation-rate peat plash lead-zinc ore Download PDFInfo
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- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/001—Flotation agents
- B03D1/002—Inorganic compounds
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- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
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- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/005—Dispersants
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/007—Modifying reagents for adjusting pH or conductivity
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- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/02—Collectors
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- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/06—Depressants
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2203/00—Specified materials treated by the flotation agents; specified applications
- B03D2203/02—Ores
- B03D2203/04—Non-sulfide ores
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Abstract
The invention discloses a flotation method of high-oxidation-rate peat plausite lead-zinc ore, which comprises the following steps: grinding ore; flotation of lead sulfide: lead sulfide concentrate is obtained through primary lead roughing and tertiary lead concentration, and the roughing tailings are subjected to primary lead scavenging; zinc sulfide flotation: performing primary roughing and primary concentration on the lead sulfide flotation tailing slurry to obtain zinc sulfide concentrate, and performing secondary zinc scavenging on the roughing tailing; zinc oxide flotation: zinc oxide concentrate is obtained from zinc sulfide flotation tailings through primary roughing and four-time concentration, and final tailings are obtained from the roughing tailings through secondary zinc scavenging. According to the invention, the flotation characteristics of sulfide ores and oxide ores are utilized to sequentially float lead-zinc sulfide ores which are easy to float, and the zinc oxide ores are floated by adjusting the potential of ore pulp, adopting a combined inhibitor to inhibit gangue and adopting a combined collecting agent, so that the problem of difficulty in separation of the zinc oxide ores is solved, a better ore separation index is obtained, the ore separation process is shortened, and the using amount of chemical agents is reduced.
Description
Technical Field
The invention relates to the technical field of metallurgy and chemical industry, in particular to a flotation and mineral separation process for lead-zinc ores.
Background
The lead-zinc ore resources in China are rich, and the proven reserves are second in the world and second to Australia. In nature, lead and zinc mainly exist in the form of sulfide ore and oxidized ore, according to the oxidation degree of lead and zinc ore, ore with the lead and zinc oxidation rate of more than 30% is called oxidized ore, ore with the lead and zinc oxidation rate of 10% -30% is called mixed ore, and ore with the lead and zinc oxidation rate of less than 10% is called sulfide ore. The zinc mineral mainly exists in the form of zinc oxide mineral and zinc sulfide mineral, and belongs to refractory lead-zinc ore.
At present, lead-zinc ore resources mainly developed in China are lead-zinc sulfide ores, and the mainstream ore dressing methods of the lead-zinc sulfide ores comprise a low-alkali process and a high-alkali process. The development of lead-zinc oxide ore resources is relatively less, the ore dressing process mainly comprises a combined heavy (magnetic) -flotation process, a combined dressing-metallurgy process, a pre-separation desliming-vulcanization flotation process and the like, and the processes have high requirements on production conditions and high production cost and are not suitable for large-scale industrial production. However, the beneficiation method of the peat board rock type lead-zinc ore is only reported, the beneficiation difficulty of the type of ore is the influence of fine mud and carbon in ore pulp on the flotation of the lead-zinc ore, and no good chemical system is provided for separating zinc oxide minerals.
Disclosure of Invention
The invention aims to solve the technical problems of high ore dressing difficulty, long ore dressing process flow, low lead and zinc ore dressing recovery rate and the like of peat board rock type lead and zinc ores and provides a flotation process for high-oxidation-rate peat board rock lead and zinc ores, which can realize high-efficiency recovery of lead and zinc sulfide ores and high-efficiency separation of fine mud, carbon and zinc oxide ores.
In order to solve the technical problems, the invention adopts the following technical scheme: a flotation method of high-oxidation-rate peat based plate rock lead-zinc ore is characterized by comprising the following steps: the lead grade of the peat coal-based plash rock lead-zinc ore is 1-1.6%, the zinc grade is 10-12%, the lead oxidation rate is 30-42%, and the zinc oxidation rate is 20-36%. The metal minerals in the ores are mainly sphalerite, and then siderite, galena, pyrite, galena, willemite and the like, a very small amount of silver minerals are occasionally seen, gangue minerals are mostly dolomite, the flotation process is carried out according to the following steps,
1) adding the ore and water into a ball mill, wherein the ore grinding concentration is 66.67%, and the ore grinding is carried out until the content of the ore with the granularity of-0.074 mm is 75-80%;
2) pouring the ground ore pulp into a flotation machine, stirring, and carrying out lead sulfide mineral roughing operation to obtain lead sulfide rough concentrate I and lead sulfide roughing tailings; the process conditions of the lead sulfide roughing operation are as follows: the used pH regulator is lime, and the dosage is 2000-4000 g/t; the inhibitor is water glass, and the dosage is 500-1000 g/t; the zinc sulfide mineral inhibitor is zinc sulfate, and the dosage is 1000-2000 g/t; the lead sulfide collecting agent is ethionamide, the dosage is 50-120g/t, the action time is 3-4min, the foaming agent is 2# oil, the dosage is 14-28g/t, and the action time is 1-2 min;
3) carrying out tertiary concentration on the lead rough concentrate obtained in the step 2) to obtain lead sulfide concentrate and three concentrated middlings, and returning the three concentrated middlings to the previous layer of operation in sequence; the lead sulfide mineral concentration process conditions are as follows: selecting I, adding lime to adjust the pH value of ore pulp to be more than or equal to 10, adding 400g/t zinc sulfate serving as a zinc sulfide mineral inhibitor, and reacting for 3-4 min; selecting II, adding lime to adjust the pH value of the ore pulp to be more than or equal to 10, adding zinc sulfide mineral inhibitor zinc sulfate 200-400g/t, and acting for 3-4 min; selecting III, adding lime to adjust the pH value of the ore pulp to be more than or equal to 10, adding 100-200g/t zinc sulfate serving as a zinc sulfide mineral inhibitor, and reacting for 3-4 min;
4) performing primary lead scavenging on the lead roughing tailings obtained in the step 2) to obtain lead sulfide scavenging middlings and lead sulfide scavenging tailings, returning the scavenging middlings to the previous layer of operation in sequence, and enabling the scavenging tailings to enter zinc sulfide roughing operation; the process conditions of lead sulfide scavenging operation are as follows: the dosage of zinc sulfate serving as a zinc sulfide inhibitor is 400-600g/t, the dosage of a lead sulfide collecting agent is 30-50g/t, and the action time is 3-4 min;
5) performing zinc sulfide roughing on the lead sulfide scavenging tailings obtained in the step 4) to obtain zinc sulfide rough concentrate and zinc sulfide roughing tailings; the process conditions of the zinc sulfide roughing operation are as follows: the dosage of lime is 700-450 g/t, the dosage of copper sulfate is 350-450g/t, the dosage of butyl xanthate is 100-150g/t, the action time is 3-4min, the dosage of 2# oil is 14-28g/t, and the action time is 1-2 min;
6) performing primary concentration on the zinc sulfide rough concentrate obtained in the step 5) to obtain zinc sulfide concentrate and middling, and sequentially returning the middling to the previous layer of operation; the process conditions of the zinc sulfide concentration operation are as follows: adding lime to adjust pH to 12 or more, and allowing the mixture to act for 2-3 min;
7) performing scavenging twice on the zinc sulfide roughing tailings obtained in the step 5) to obtain scavenged middlings and scavenged tailings, wherein the scavenged middlings sequentially return to the previous layer of operation, and the scavenged tailings sequentially enter the next flotation operation; the zinc sulfide scavenging operation process conditions are as follows: adding 150-250g/t of activating agent copper sulfate and 50-70g/t of collecting agent butyl xanthate into zinc sulfide scavenging I, and operating for 3-4 min; adding 50-150g/t of activating agent copper sulfate and 20-40g/t of collecting agent butyl xanthate into the scavenging II, and operating for 3-4 min;
8) performing zinc oxide roughing on the tailings obtained in the second scavenging step 7) to obtain zinc oxide rough concentrate and zinc oxide roughing tailings; the process conditions of the zinc oxide roughing operation are as follows: adding 2000g/t of regulator sodium carbonate, adding 1500g/t of combined inhibitor water glass and 600g/t of sodium hexametaphosphate with the dosages of 700 + 1500g/t and 400 + 600g/t respectively, adding 7000g/t of vulcanizing agent sodium sulfide, adding 600g/t of activating agent ammonium sulfate, adding 400 + 400g/t of combined collecting agents octadecylamine and hexadecylamine with the dosages of 200 + 400g/t and 200 + 400g/t respectively, and allowing the reaction time to be 3-4 min; adding 7-21g/t of 2# oil, and acting for 1-2 min;
9) carrying out four times of concentration on the zinc oxide rough concentrate obtained in the step 8) to obtain zinc oxide concentrate and concentrated middlings, and returning the concentrated middlings to the previous layer of operation in sequence; the zinc oxide concentration operation process conditions are as follows: selecting I, adding 700-1500g/t of sodium carbonate, adding 600g/t of combined inhibitor water glass and 400g/t of combined inhibitor sodium hexametaphosphate, and reacting for 3-4 min; selecting II, adding 400g/t of sodium carbonate, adding 400g/t of water glass and 300g/t of sodium hexametaphosphate as combined inhibitors, wherein the dosages are respectively 400g/t and 100g/t, and the action time is 3-4 min; selecting III, adding 200-400g/t of sodium carbonate, adding 300-150 g/t of combined inhibitor water glass and 50-150g/t of combined inhibitor sodium hexametaphosphate, and reacting for 3-4 min; selecting IV, adding 100g/t of sodium carbonate, adding water glass and sodium hexametaphosphate as combined inhibitors, wherein the dosage is 50-150g/t and 40-60g/t respectively, and the action time is 3-4 min;
10) performing secondary scavenging on the zinc oxide roughing tailings obtained in the step 9), returning the obtained scavenging middlings to the previous layer of operation in sequence, and discharging scavenged II tailings serving as final flotation tailings into a tailing pond; the process conditions of the zinc oxide scavenging operation are as follows: adding 4000g/t of sodium sulfide as a vulcanizing agent, 2000g/t of ammonium sulfate as an activating agent, 300g/t of ammonium sulfate as a scavenging agent, adding 400g/t of octadecylamine and 400g/t of hexadecylamine as combined collecting agents, wherein the use amounts of 200 and 400g/t of 200 respectively, and the action time is 3-4 min; adding 1000-2000g/t of sodium sulfide vulcanizing agent into the scavenging II, adding 50-150g/t of ammonium sulfate as an activating agent, and adding 300g/t of octadecylamine and 300g/t of hexadecylamine as combined collecting agents, wherein the use amounts are 100-300g/t and 100-300g/t respectively, and the action time is 3-4 min.
The invention is mainly characterized in that: firstly, the invention utilizes the floating characteristics of different minerals to float lead and zinc sulfide which are easy to float out in sequence, and the flotation tailings directly float zinc oxide minerals, thereby shortening the flotation process flow and reducing the production cost.
Secondly, the fine mud in the ore pulp is dispersed by using a regulator sodium carbonate, and the function of regulating the electric potential of the ore pulp is achieved; and then, the positively charged fine slime in the ore pulp is adsorbed and precipitated by utilizing anions in the combined inhibitor water glass and sodium hexametaphosphate through electrostatic adsorption, and the fine slime is dropped from the surface of the zinc oxide, so that the problem that the slime covers the surface of the zinc oxide mineral to cause the zinc oxide mineral to be difficult to capture by the collecting agent is solved.
Thirdly, the surface of the magnesium oxide is vulcanized and activated by utilizing sodium sulfide serving as a vulcanizing agent and ammonium sulfate serving as an activating agent, and the zinc oxide mineral is collected by utilizing the synergistic effect of octadecylamine and hexadecylamine serving as combined anion collecting agents, so that the zinc oxide mineral is floated out, the zinc oxide mineral is effectively collected, the separation of the zinc oxide mineral and gangue mineral is well realized, and the problem that the zinc oxide mineral is difficult to select and collect is solved. The beneficiation method of the invention not only reduces the beneficiation production cost, but also improves the beneficiation recovery rate of zinc minerals, solves the beneficiation problem of peat porphyry type lead-zinc ores, and can increase the economic benefit for enterprises.
Therefore, the method of the invention can avoid the pre-desliming process of the zinc sulfide scavenging tailings, thereby shortening the process flow and obtaining zinc oxide concentrate by directly floating zinc oxide from the zinc sulfide scavenging tailings and carrying out concentration for four times.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The invention will be further illustrated by the following specific examples in conjunction with figure 1:
example 1, ore properties: the lead grade was 1.11%, the zinc grade was 11.33%, the lead oxidation rate was 41.49%, and the zinc oxidation rate was 35.21%. The metal minerals in the ores are mainly sphalerite, and secondly calamine, galena, pyrite, galena, willemite and the like, and the trace minerals are rare silver minerals, and the gangue minerals are mostly dolomite.
The method comprises the following steps:
1) adding the ore and water into a ball mill, wherein the ore grinding concentration is 66.67%, and the ore grinding is carried out until the content of the ore with the granularity of-0.074 mm is 75%;
2) pouring the ground ore pulp into a flotation machine, stirring, and carrying out lead sulfide mineral roughing operation to obtain lead sulfide rough concentrate I and lead sulfide roughing tailings; the process conditions of the lead sulfide roughing operation are as follows: the used pH regulator is lime with the dosage of 3000g/t, and the zinc sulfide mineral inhibitor is zinc sulfate with the dosage of 1000 g/t. The lead sulfide collecting agent is ethionamide, the dosage is 80g/t, the action time is 3-4min, the foaming agent is 2# oil, the dosage is 21g/t, and the action time is 1-2 min;
3) carrying out tertiary concentration on the lead rough concentrate obtained in the step 2) to obtain lead sulfide concentrate and three concentrated middlings, and returning the three concentrated middlings to the previous layer of operation in sequence; the lead sulfide mineral concentration process conditions are as follows: selecting I, adding lime to adjust the pH value of ore pulp to be more than or equal to 10, adding zinc sulfide mineral inhibitor zinc sulfate 500g/t, and acting for 3-4 min; selecting II, adding lime to adjust the pH value of the ore pulp to be more than or equal to 10, adding zinc sulfide mineral inhibitor zinc sulfate 300g/t, and acting for 3-4 min; selecting III, adding lime to adjust the pH value of the ore pulp to be more than or equal to 10, adding 100g/t zinc sulfate serving as a zinc sulfide mineral inhibitor, and acting for 3-4 min;
4) performing primary lead scavenging on the lead roughing tailings obtained in the step 2) to obtain lead sulfide scavenging middlings and lead sulfide scavenging tailings, returning the scavenging middlings to the previous layer of operation in sequence, and enabling the scavenging tailings to enter zinc sulfide roughing operation; the process conditions of lead sulfide scavenging operation are as follows: the using amount of zinc sulfate serving as a zinc sulfide inhibitor is 500g/t, the using amount of a lead sulfide collecting agent is 40g/t, and the acting time is 3-4 min;
5) performing zinc sulfide roughing on the lead sulfide scavenging tailings obtained in the step 4) to obtain zinc sulfide rough concentrate and zinc sulfide roughing tailings; the process conditions of the zinc sulfide roughing operation are as follows: the dosage of lime is 1000g/t, the dosage of copper sulfate is 400g/t, the dosage of butyl xanthate is 120g/t, the action time is 3-4min, the dosage of 2# oil is 21g/t, and the action time is 1-2 min;
6) and 5) carrying out primary concentration on the zinc sulfide rough concentrate obtained in the step 5) to obtain zinc sulfide concentrate and middling, and sequentially returning the middling to the previous layer for operation. The process conditions of the zinc sulfide concentration operation are as follows: adding lime to adjust pH to 12 or more, and allowing the mixture to act for 2-3 min;
7) scavenging the zinc sulfide roughing tailings obtained in the step 5) twice to obtain scavenged middlings and scavenged tailings, wherein the scavenged middlings sequentially return to the previous layer of operation, and the scavenged tailings sequentially enter the next flotation operation. The zinc sulfide scavenging operation process conditions are as follows: adding 200g/t of activating agent copper sulfate and 60g/t of collecting agent butyl xanthate into zinc sulfide scavenging I, and operating for 3-4 min; adding 100g/t of activating agent copper sulfate and 30g/t of collecting agent butyl xanthate into the scavenging II, and operating for 3-4 min;
8) and (3) performing zinc oxide roughing on the tailings obtained in the second scavenging step in the step 7) to obtain zinc oxide rough concentrate and zinc oxide roughing tailings. The process conditions of the zinc oxide roughing operation are as follows: adding 2000g/t of sodium carbonate serving as a regulator, adding water glass serving as a combined inhibitor and sodium hexametaphosphate, wherein the dosage is 1000g/t and 500g/t respectively, adding 6000g/t of sodium sulfide serving as a vulcanizing agent, adding 500g/t of ammonium sulfate serving as an activating agent, adding octadecylamine and hexadecylamine serving as combined collectors, wherein the dosage is 300g/t and 300g/t respectively, the action time is 3-4min, adding 14g/t of 2# oil, and the action time is 1-2 min;
9) and (3) carrying out four times of concentration on the zinc oxide rough concentrate obtained in the step 8) to obtain zinc oxide concentrate and concentrated middlings, and returning the concentrated middlings to the previous layer of operation in sequence. The zinc oxide concentration operation process conditions are as follows: selecting I, adding 1000g/t of sodium carbonate, adding water glass serving as a combined inhibitor and sodium hexametaphosphate, wherein the dosage is 500g/t and 300g/t respectively, and the action time is 3-4 min; selecting II, adding 500g/t of sodium carbonate, adding 300g/t of combined inhibitor water glass and 200g/t of combined inhibitor sodium hexametaphosphate, and acting for 3-4 min; selecting III, adding 300g/t of sodium carbonate, adding water glass and sodium hexametaphosphate as combined inhibitors, wherein the dosage is 200g/t and 100g/t respectively, and the action time is 3-4 min; selecting IV, adding 200g/t of sodium carbonate, adding water glass and sodium hexametaphosphate as combined inhibitors, wherein the dosage is 100g/t and 50g/t respectively, and the action time is 3-4 min;
10) and (3) carrying out secondary scavenging on the zinc oxide roughing tailings obtained in the step 8), returning the obtained scavenging middlings to the previous layer of operation in sequence, and discharging scavenged II tailings serving as final flotation tailings into a tailing pond. The process conditions of the zinc oxide scavenging operation are as follows: adding 3000g/t of vulcanizing agent sodium sulfide into the scavenging I, adding 200g/t of activating agent ammonium sulfate, adding 200g/t of combined collecting agents octadecylamine and hexadecylamine, wherein the use amounts are 200g/t and 200g/t respectively, and the action time is 3-4 min; adding 1500g/t of vulcanizing agent sodium sulfide into the scavenging II, adding 100g/t of activating agent ammonium sulfate, adding 100g/t of combined collecting agents octadecylamine and hexadecylamine, wherein the use amounts are 100g/t and 100g/t respectively, and the acting time is 3-4 min.
Comparative condition 1: the flotation conditions and the process of the lead-zinc sulfide ore are the same as those of the invention, and the flotation process of the zinc oxide ore is to desliming in advance, and then sodium sulfide is used for sulfurization, a single inhibitor sodium hexametaphosphate is used for inhibiting gangue minerals, a single collector dodecylamine is used for collecting zinc oxide minerals, and No. 2 oil is used as a foaming agent.
The flotation results are shown in table 1:
TABLE 1 flotation test index (wt%)
As can be seen from table 1, when the lead-zinc ore is treated by the method of the present invention, under the conditions that the raw ore contains 1.11% of lead, 11.33% of zinc, 41.49% of lead oxidation rate and 35.21% of zinc oxidation rate, the lead grade of lead sulfide concentrate is 43.27%, the lead recovery rate is 41.19%, the zinc grade of zinc sulfide concentrate is 56.59%, the zinc recovery rate is 67.24%, the zinc grade of zinc oxide concentrate is 23.43%, and the zinc recovery rate is 22.67%. Compared with the traditional method, the method improves the zinc oxide concentrate grade by 0.31 percent, and improves the recovery rate by 5.72 percent. The method can be used for efficiently recovering the zinc oxide with the oxidation rate of 35.21 percent in the lead-zinc ore, and has remarkable advantages.
Example 2, ore properties: the lead grade is 1.54%, the zinc grade is 10.15%, the lead oxidation rate is 30.46%, and the zinc oxidation rate is 20.02%. The metal minerals in the ores are mainly sphalerite, and secondly calamine, galena, pyrite, galena, willemite and the like, and the trace minerals are rare silver minerals, and the gangue minerals are mostly dolomite.
The method comprises the following steps:
1) adding the ore and water into a ball mill, wherein the ore grinding concentration is 66.67%, and the ore grinding is carried out until the content of the ore with the granularity of-0.074 mm is 80%;
2) pouring the ground ore pulp into a flotation machine, stirring, and carrying out lead sulfide mineral roughing operation to obtain lead sulfide rough concentrate I and lead sulfide roughing tailings; the process conditions of the lead sulfide roughing operation are as follows: the used pH regulator is lime with the dosage of 4000g/t, and the zinc sulfide mineral inhibitor is zinc sulfate with the dosage of 800 g/t. The lead sulfide collecting agent is ethionamide, the dosage is 70g/t, the action time is 3-4min, the foaming agent is 2# oil, the dosage is 21g/t, and the action time is 1-2 min;
3) carrying out tertiary concentration on the lead rough concentrate obtained in the step 2) to obtain lead sulfide concentrate and three concentrated middlings, and returning the three concentrated middlings to the previous layer of operation in sequence; the lead sulfide mineral concentration process conditions are as follows: selecting I, adding lime to adjust the pH value of ore pulp to be more than or equal to 10, adding zinc sulfide mineral inhibitor zinc sulfate 400g/t, and acting for 3-4 min; selecting II, adding lime to adjust the pH value of the ore pulp to be more than or equal to 10, adding zinc sulfide mineral inhibitor zinc sulfate 200g/t, and acting for 3-4 min; selecting III, adding lime to adjust the pH value of the ore pulp to be more than or equal to 10, adding zinc sulfide mineral inhibitor zinc sulfate 50g/t, and acting for 3-4 min;
4) performing primary lead scavenging on the lead roughing tailings obtained in the step 2) to obtain lead sulfide scavenging middlings and lead sulfide scavenging tailings, returning the scavenging middlings to the previous layer of operation in sequence, and enabling the scavenging tailings to enter zinc sulfide roughing operation; the process conditions of lead sulfide scavenging operation are as follows: the using amount of zinc sulfate serving as a zinc sulfide inhibitor is 400g/t, the using amount of a lead sulfide collecting agent is 30g/t, and the acting time is 3-4 min;
5) performing zinc sulfide roughing on the lead sulfide scavenging tailings obtained in the step 4) to obtain zinc sulfide rough concentrate and zinc sulfide roughing tailings; the process conditions of the zinc sulfide roughing operation are as follows: lime dosage is 1500g/t, copper sulfate dosage is 300g/t, butyl xanthate dosage is 120g/t, action time is 3-4min, 2#The oil dosage is 28g/t, and the action time is 1-2 min;
6) and 5) carrying out primary concentration on the zinc sulfide rough concentrate obtained in the step 5) to obtain zinc sulfide concentrate and middling, and sequentially returning the middling to the previous layer for operation. The process conditions of the zinc sulfide concentration operation are as follows: adding lime to adjust pH to 12 or more, and allowing the mixture to act for 2-3 min;
7) scavenging the zinc sulfide roughing tailings obtained in the step 5) twice to obtain scavenged middlings and scavenged tailings, wherein the scavenged middlings sequentially return to the previous layer of operation, and the scavenged tailings sequentially enter the next flotation operation. The zinc sulfide scavenging operation process conditions are as follows: adding 150g/t of activating agent copper sulfate and 40g/t of collecting agent butyl xanthate into zinc sulfide scavenging I, and operating for 3-4 min; 70g/t of activating agent copper sulfate and 20g/t of collecting agent butyl xanthate are added into the scavenging II, and the operation time is 3-4 min;
8) and (3) performing zinc oxide roughing on the tailings obtained in the second scavenging step in the step 7) to obtain zinc oxide rough concentrate and zinc oxide roughing tailings. The process conditions of the zinc oxide roughing operation are as follows: adding 1500g/t of sodium carbonate serving as a regulator, adding 800g/t and 400g/t of sodium hexametaphosphate serving as a combined inhibitor, adding 5000g/t of sodium sulfide serving as a vulcanizing agent, 300g/t of ammonium sulfate serving as an activating agent, adding 200g/t and 200g/t of octadecylamine serving as a combined collector and hexadecylamine serving as a combined collector, reacting for 3-4min, adding 7g/t of 2# oil, and reacting for 1-2 min;
9) and (3) carrying out four times of concentration on the zinc oxide rough concentrate obtained in the step 8) to obtain zinc oxide concentrate and concentrated middlings, and returning the concentrated middlings to the previous layer of operation in sequence. The zinc oxide concentration operation process conditions are as follows: selecting I, adding 800g/t of sodium carbonate, adding water glass serving as a combined inhibitor and sodium hexametaphosphate, wherein the dosage is 400g/t and 200g/t respectively, and the action time is 3-4 min; selecting II, adding 400g/t of sodium carbonate, adding 200g/t of combined inhibitor water glass and 150g/t of combined inhibitor sodium hexametaphosphate, and acting for 3-4 min; selecting III, adding 200g/t of sodium carbonate, adding combined inhibitor water glass and sodium hexametaphosphate, wherein the dosage is 150g/t and 70g/t respectively, and the action time is 3-4 min; selecting IV, adding 100g/t of sodium carbonate, adding a combined inhibitor of water glass and sodium hexametaphosphate, wherein the dosage is 50g/t and 30g/t respectively, and the action time is 3-4 min;
10) and (3) carrying out secondary scavenging on the zinc oxide roughing tailings obtained in the step 8), returning the obtained scavenging middlings to the previous layer of operation in sequence, and discharging scavenged II tailings serving as final flotation tailings into a tailing pond. The process conditions of the zinc oxide scavenging operation are as follows: adding 2000g/t of vulcanizing agent sodium sulfide into the scavenging I, adding 150g/t of activating agent ammonium sulfate, adding 150g/t of combined collecting agents octadecylamine and hexadecylamine, wherein the use amounts are 150g/t and 150g/t respectively, and the acting time is 3-4 min; and adding 1000g/t of sodium sulfide serving as a vulcanizing agent into the scavenging II, adding 50g/t of ammonium sulfate serving as an activating agent, adding 50g/t of octadecylamine and 50g/t of hexadecylamine serving as combined collecting agents, and reacting for 3-4 min.
Comparative condition 2: the flotation conditions and the process of the lead-zinc sulfide ore are the same as those of the invention, and the flotation process of the zinc oxide ore is to desliming in advance, and then sodium sulfide is used for sulfurization, a single inhibitor sodium hexametaphosphate is used for inhibiting gangue minerals, a single collector dodecylamine is used for collecting zinc oxide minerals, and No. 2 oil is used as a foaming agent.
The flotation results are shown in table 1:
TABLE 2 flotation test index (wt%)
As can be seen from table 2, when the lead-zinc ore is treated by the method of the present invention, under the conditions that the raw ore contains 1.54% of lead, 10.26% of zinc, 30.46% of lead oxidation rate and 20.02% of zinc oxidation rate, the lead grade of the lead sulfide concentrate is 47.53%, the lead recovery rate is 39.31%, the zinc grade of the zinc sulfide concentrate is 55.25%, the zinc recovery rate is 80.68%, the zinc grade of the zinc oxide concentrate is 25.16%, and the zinc recovery rate is 13.12%. Compared with the traditional method, the zinc grade of the zinc oxide concentrate is basically unchanged, and the zinc recovery rate is improved by 5.55 percent. The method can be used for efficiently recovering the zinc oxide with the oxidation rate of 20.02 percent in the lead-zinc ore, and has remarkable advantages.
The present invention has been described in detail, and it should be understood that the detailed description and specific examples, while indicating the preferred embodiment of the invention, are intended for purposes of illustration only and are not intended to limit the scope of the invention.
Claims (3)
1. A flotation method of high-oxidation-rate peat based plate rock lead-zinc ore is characterized by comprising the following steps: the method comprises the following steps of (1),
1) adding ore and water into a ball mill for grinding;
2) pouring the ground ore pulp into a flotation machine, stirring, and carrying out lead sulfide mineral roughing operation to obtain lead sulfide rough concentrate I and lead sulfide roughing tailings; the process conditions of the lead sulfide roughing operation are as follows: the used pH regulator is lime, and the dosage is 2000-4000 g/t; the inhibitor is water glass, and the dosage is 500-1000 g/t; the zinc sulfide mineral inhibitor is zinc sulfate, and the dosage is 1000-2000 g/t; the lead sulfide collecting agent is ethionamide, the dosage is 50-120g/t, the action time is 3-4min, the foaming agent is 2# oil, the dosage is 14-28g/t, and the action time is 1-2 min;
3) carrying out tertiary concentration on the lead rough concentrate obtained in the step 2) to obtain lead sulfide concentrate and three concentrated middlings, and returning the three concentrated middlings to the previous layer of operation in sequence; the lead sulfide mineral concentration process conditions are as follows: selecting I, adding lime to adjust the pH value of ore pulp to be more than or equal to 10, adding 400g/t zinc sulfate serving as a zinc sulfide mineral inhibitor, and reacting for 3-4 min; selecting II, adding lime to adjust the pH value of the ore pulp to be more than or equal to 10, adding zinc sulfide mineral inhibitor zinc sulfate 200-400g/t, and acting for 3-4 min; selecting III, adding lime to adjust the pH value of the ore pulp to be more than or equal to 10, adding 100-200g/t zinc sulfate serving as a zinc sulfide mineral inhibitor, and reacting for 3-4 min;
4) performing primary lead scavenging on the lead roughing tailings obtained in the step 2) to obtain lead sulfide scavenging middlings and lead sulfide scavenging tailings, returning the scavenging middlings to the previous layer of operation in sequence, and enabling the scavenging tailings to enter zinc sulfide roughing operation; the process conditions of lead sulfide scavenging operation are as follows: the dosage of zinc sulfate serving as a zinc sulfide inhibitor is 400-600g/t, the dosage of a lead sulfide collecting agent is 30-50g/t, and the action time is 3-4 min;
5) performing zinc sulfide roughing on the lead sulfide scavenging tailings obtained in the step 4) to obtain zinc sulfide rough concentrate and zinc sulfide roughing tailings; the process conditions of the zinc sulfide roughing operation are as follows: the dosage of lime is 700-450 g/t, the dosage of copper sulfate is 350-450g/t, the dosage of butyl xanthate is 100-150g/t, the action time is 3-4min, the dosage of 2# oil is 14-28g/t, and the action time is 1-2 min;
6) performing primary concentration on the zinc sulfide rough concentrate obtained in the step 5) to obtain zinc sulfide concentrate and middling, and sequentially returning the middling to the previous layer of operation; the process conditions of the zinc sulfide concentration operation are as follows: adding lime to adjust pH to 12 or more, and allowing the mixture to act for 2-3 min;
7) performing scavenging twice on the zinc sulfide roughing tailings obtained in the step 5) to obtain scavenged middlings and scavenged tailings, wherein the scavenged middlings sequentially return to the previous layer of operation, and the scavenged tailings sequentially enter the next flotation operation; the zinc sulfide scavenging operation process conditions are as follows: adding 150-250g/t of activating agent copper sulfate and 50-70g/t of collecting agent butyl xanthate into zinc sulfide scavenging I, and operating for 3-4 min; adding 50-150g/t of activating agent copper sulfate and 20-40g/t of collecting agent butyl xanthate into the scavenging II, and operating for 3-4 min;
8) performing zinc oxide roughing on the tailings obtained in the second scavenging step 7) to obtain zinc oxide rough concentrate and zinc oxide roughing tailings; the process conditions of the zinc oxide roughing operation are as follows: adding 2000g/t of regulator sodium carbonate, adding 1500g/t of combined inhibitor water glass and 600g/t of sodium hexametaphosphate with the dosages of 700 + 1500g/t and 400 + 600g/t respectively, adding 7000g/t of vulcanizing agent sodium sulfide, adding 600g/t of activating agent ammonium sulfate, adding 400 + 400g/t of combined collecting agents octadecylamine and hexadecylamine with the dosages of 200 + 400g/t and 200 + 400g/t respectively, and allowing the reaction time to be 3-4 min; adding 7-21g/t of 2# oil, and acting for 1-2 min;
9) carrying out four times of concentration on the zinc oxide rough concentrate obtained in the step 8) to obtain zinc oxide concentrate and concentrated middlings, and returning the concentrated middlings to the previous layer of operation in sequence; the zinc oxide concentration operation process conditions are as follows: selecting I, adding 700-1500g/t of sodium carbonate, adding 600g/t of combined inhibitor water glass and 400g/t of combined inhibitor sodium hexametaphosphate, and reacting for 3-4 min; selecting II, adding 400g/t of sodium carbonate, adding 400g/t of water glass and 300g/t of sodium hexametaphosphate as combined inhibitors, wherein the dosages are respectively 400g/t and 100g/t, and the action time is 3-4 min; selecting III, adding 200-400g/t of sodium carbonate, adding 300-150 g/t of combined inhibitor water glass and 50-150g/t of combined inhibitor sodium hexametaphosphate, and reacting for 3-4 min; selecting IV, adding 100g/t of sodium carbonate, adding water glass and sodium hexametaphosphate as combined inhibitors, wherein the dosage is 50-150g/t and 40-60g/t respectively, and the action time is 3-4 min;
10) performing secondary scavenging on the zinc oxide roughing tailings obtained in the step 9), returning the obtained scavenging middlings to the previous layer of operation in sequence, and discharging scavenged II tailings serving as final flotation tailings into a tailing pond; the process conditions of the zinc oxide scavenging operation are as follows: adding 4000g/t of sodium sulfide as a vulcanizing agent, 2000g/t of ammonium sulfate as an activating agent, 300g/t of ammonium sulfate as a scavenging agent, adding 400g/t of octadecylamine and 400g/t of hexadecylamine as combined collecting agents, wherein the use amounts of 200 and 400g/t of 200 respectively, and the action time is 3-4 min; adding 1000-2000g/t of sodium sulfide vulcanizing agent into the scavenging II, adding 50-150g/t of ammonium sulfate as an activating agent, and adding 300g/t of octadecylamine and 300g/t of hexadecylamine as combined collecting agents, wherein the use amounts are 100-300g/t and 100-300g/t respectively, and the action time is 3-4 min.
2. The method of claim 1 for flotation of lead zinc ore from high oxidation rate peat based panels, comprising: in the step 1), the concentration of ore grinding is 66.67%, and the ore grinding is carried out until the content of ore grinding with the granularity of-0.074 mm is 75-80%.
3. The method of claim 1 for flotation of lead zinc ore from high oxidation rate peat based panels, comprising: lead grade is 1-1.6%, zinc grade is 10-12%, lead oxidation rate is 30-42%, and zinc oxidation rate is 20-36%.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8910083D0 (en) * | 1989-05-03 | 1989-06-21 | Minerals Concepts Research Ltd | Metallurgical process for upgrading zinc concentrates |
| CN109013049A (en) * | 2018-06-21 | 2018-12-18 | 中国恩菲工程技术有限公司 | The method for handling Pb-Zn deposits |
| CN109482361A (en) * | 2018-12-12 | 2019-03-19 | 北京矿冶科技集团有限公司 | A kind of method that lead-zinc sulphur oxygen synchronizes flotation |
| CN111530633A (en) * | 2020-04-27 | 2020-08-14 | 西部矿业股份有限公司 | Novel composite collecting agent for recovering zinc oxide from peat plaza lead zinc oxide ore, preparation method and application |
| CN112718252A (en) * | 2020-12-15 | 2021-04-30 | 长沙矿山研究院有限责任公司 | Flotation recovery method for high-calcium-magnesium high-argillaceous mixed lead-zinc ore |
-
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- 2021-06-19 CN CN202110681818.4A patent/CN113457852A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8910083D0 (en) * | 1989-05-03 | 1989-06-21 | Minerals Concepts Research Ltd | Metallurgical process for upgrading zinc concentrates |
| CN109013049A (en) * | 2018-06-21 | 2018-12-18 | 中国恩菲工程技术有限公司 | The method for handling Pb-Zn deposits |
| CN109482361A (en) * | 2018-12-12 | 2019-03-19 | 北京矿冶科技集团有限公司 | A kind of method that lead-zinc sulphur oxygen synchronizes flotation |
| CN111530633A (en) * | 2020-04-27 | 2020-08-14 | 西部矿业股份有限公司 | Novel composite collecting agent for recovering zinc oxide from peat plaza lead zinc oxide ore, preparation method and application |
| CN112718252A (en) * | 2020-12-15 | 2021-04-30 | 长沙矿山研究院有限责任公司 | Flotation recovery method for high-calcium-magnesium high-argillaceous mixed lead-zinc ore |
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